Use of titania or zirconia in the preparation of tertiary butyl alcohol from tertiary butyl alcohol from tertiary butyl hydroperoxide

Abstract: A method for preparing tertiary butyl alcohol wherein a feedstock comprising a solvent solution of tertiary butyl hydroperoxide in tertiary butyl alcohol or a mixture of tertiary butyl alcohol with isobutane is charged to a hydroperoxide decomposition reaction zone containing a catalytically effective amount of a hydroperoxide decomposition catalyst consisting essentially of titania or zirconia and is brought into contact with the catalyst in liquid phase under hydroperoxide decomposition reaction conditions to convert the tertiary butyl hydroperoxide to decomposition products, principally tertiary butyl alcohol.

Description: This invention relates to the catalytic decomposition of tertiary butyl hydroperoxide (TBHP). More particularly, this invention relates to a method for the preparation of tertiary butyl alcohol (TBA) by the catalytic decomposition of tertiary butyl hydroperoxide. Still more particularly, this invention relates to a method wherein titania or zirconia is used to catalyze the substantially selective decomposition of tertiary butyl hydroperoxide to tertiary butyl alcohol. It is known to react isobutane with oxygen, either thermally or catalytically, to form a peroxidation reaction product wherein the principal peroxide that is formed is tertiary butyl hydroperoxide. It is also known to thermally or catalytically decompose the tertiary butyl hydroperoxide to form tertiary butyl alcohol. Sanderson et al. disclose the use of a variety of catalysts for the decomposition of tertiary butyl hydroperoxide in a series of U. S. patents, including a catalyst composed of unsupported nickel, copper, chromia and iron (U. S. Patent No. 4,704,482), a catalyst composed of iron, copper, chromia and cobalt (U. S. Patent No. 4,705,903), a catalyst composed of a base treated hydrogenation catalyst from groups VIA or VIII of the Periodic Table (U. S. Patent No. 4,742,179), a catalyst consisting essentially of nickel, copper, chromium and barium (U. S. Patent No. 4,873,380), a catalyst composed of a metal phthalocyanine promoted with a rhenium compound (U. S. Patent No. 4,910,349), a catalyst composed of a base promoted metal phthalocyanine compound (U. S. Patent No. 4,912,269), a catalyst composed of a soluble ruthenium compound promoted with a bidentate ligand (U. S. Patent No. 4,912,033), a catalyst composed of a metal porphine such as iron (III) or manganese (III) promoted with an alkyl thiol or an amine, a catalyst composed of an imidazole promoted metal phthalocyanine compound (U. S. Patent No. 4,912,266), (U. S. Patent No. 4,922,034), a catalyst composed of a metal phthalocyanine promoted with a thiol and a free radical inhibitor (U. S. Patent No. 4,922,035), a catalyst composed of a borate promoted metal phthalocyanine (U. S. Patent No. 4,922,036), or a catalyst composed of a soluble ruthenium compound and an iron compound such as an acetate, a borate, a bromide, a chloride, a 1,3-propanedionate , a 2-ethyl-hexanoate, an iodide, a nitrate, a 2,4-pentanedionate, a perchlorate or a sulfate (U. S. Patent No. 5,025,113). As stated, when isobutane is reacted with molecular oxygen, the principal products of the reaction are tertiary butyl alcohol and tertiary butyl hydroperoxide. However, minor amounts of other contaminants are also formed. A minor amount of water will be formed, which will normally amount to about 0.5 to 1 wt.% of the reactor effluent. The amount of byproduct water that is produced is a function of the severity of the reaction conditions employed and will tend to increase as the severity of the reaction conditions is increased. As indicated, tertiary butyl hydroperoxide is useful as a raw material for the manufacture of tertiary butyl alcohol. The tertiary butyl alcohol can be formed by catalytic decomposition of the tertiary butyl hydroperoxide. US-A-3,472,876 discloses a process wherein an oxygen-containing gas was charged to a reactor containing isobutane and an oxidation catalyst to provide a reaction mixture comprising tertiary butyl alcohol, tertiary butyl hydroperoxide, acetone, and tertiary butyl ether. The reported results in the patent indicate that there was a comparatively low rate of conversion and a comparatively poor selectivity of the reaction to tertiary butyl alcohol. There is a need for a catalytic decomposition of tertiary butyl hydroperoxide to tertiary alcohol at a higher conversion rate and an improved selectivity over the prior art. Titanium dioxide (titania) and zirconium dioxide (zirconia) are rugged, stable compounds that are useful as supports for catalytically active metals. It has been surprisingly discovered in accordance with the present invention that titania and zirconia effectively and substantially selectively catalyze the decomposition of tertiary butyl hydroperoxide to tertiary butyl alcohol. Thus, in accordance with the present invention, a solvent solution of a tertiary butyl hydroperoxide charge stock is brought into contact with a catalytically effective amount of titania or zirconia in a hydroperoxide decomposition reaction zone in liquid phase, preferably with agitation, to convert the tertiary butyl hydroperoxide to decomposition products, principally tertiary butyl alcohol. The hydroperoxide decomposition catalyst consists essentially of titania or zirconia. Tertiary butyl alcohol is recovered from the products of the hydroperoxide decomposition reaction. The tertiary butyl alcohol will not be the only decomposition product that is formed. Minor amounts of other oxygen-containing materials such as those listed above will also be formed. The tertiary butyl alcohol that is recovered from the decomposition reaction mixture will be contaminated with the oxygenated impurities. The starting materials for the process of the present invention are a tertiary butyl hydroperoxide feedstock and titania or zirconia. The Tertiary Butyl Hydroperoxide Feedstock The tertiary butyl hydroperoxide charge stock may comprise an isobutane oxidation product wherein the tertiary butyl hydroperoxide is dissolved in a mixture of isobutane and tertiary butyl alcohol or may comprise an isobutane oxidation product enriched by the addition of tertiary butyl alcohol, such that the solution of tertiary butyl alcohol in the mixture of isobutane with tertiary butyl alcohol contains from 5 to 30 wt.% of tertiary butyl hydroperoxide. A surprising and unexpected increase in the yield of tertiary butyl alcohol is obtained with a feedstock comprising a mixture of isobutane with tertiary butyl alcohol. Alternatively, the isobutane reaction product may be charged to a distillation zone where unreacted isobutane is removed as a distillate fraction for recycle to thereby provide a solution of tertiary butyl hydroperoxide in tertiary butyl alcohol containing 5 to 30 wt.% of tertiary butyl hydroperoxide. The Catalyst The hydroperoxide decomposition catalyst to be used in accordance with the present invention consists essentially of titania, zirconia or a mixture thereof. Pelleted catalyst is preferred. Catalytic Decomposition of Tertiary Butyl Hydroperoxide The process of the present invention may be conducted batchwise in kettles or by continuously passing the reactants through a tubular reactor. The catalytic decomposition of the tertiary butyl hydroperoxide is preferably conducted at a temperature within the range of 20° to 250°C, preferably 60° to 120°C, and more preferably at a temperature within the range of 80° to 100°C. The reaction is preferably conducted at a pressure sufficient to keep the reactants and the reaction products in liquid phase. A pressure of 0.1 to 7 MPa (0 to 1,000 psig) may be used, if desired. Flow rates of the charge solution to the reaction zone should be adjusted in order to provide an appropriate contact time within the reactor. In a batch process, the holding time may suitably be from 0.5 to 10 hours, and more preferably 1 to 3 hours. In accordance with a preferred embodiment of the present invention, isobutane is reacted with oxygen in an oxidation zone under oxidation reaction conditions including a temperature of 135° to 155°C., a pressure of 2.1 to 5.6 MPa (300 to 800 psig), and a holding time of 2 to 6 hours to provide an initial oxidation reaction product comprising unreacted isobutane, tertiary butyl hydroperoxide, tertiary butyl alcohol, and oxygen-containing by-products. The initial oxidation reaction product is then used as the tertiary butyl hydroperoxide charge stock of the present invention. If the concentration of tertiary butyl hydroperoxide in the tertiary butyl hydroperoxide charge stock is more than 30 wt.% of the initial oxidation reaction product, the initial oxidation reaction product can be diluted with an amount of tertiary butyl alcohol sufficient to lower the concentration of the tertiary butyl hydroperoxide to a desired percentage, to provide, for example, a tertiary butyl hydroperoxide charge stock containing from 15 to 25 wt.% of tertiary butyl hydroperoxide. Alternatively, the initial oxidation reaction product may be fractionated in any appropriate manner (e.g., by distillation in a distillation zone) to remove the isobutane therefrom for recycle and to provide a solution of tertiary butyl hydroperoxide and tertiary butyl alcohol which will normally contain from 5 to 30 wt.% of tertiary butyl hydroperoxide. In a continuous process, the solution of tertiary butyl hydroperoxide in tertiary butyl alcohol is charged to a catalytic hydroperoxide decomposition zone where it is brought into contact with pelleted titania or zirconia to substantially selectively convert the tertiary butyl hydroperoxide to tertiary butyl alcohol with high yields and selectivities. When the process of the present invention is practiced in a continuous manner by continuously charging the tertiary butyl hydroperoxide charge stock to a reactor containing a fixed bed of pelleted hydroperoxide decomposition catalyst, the space velocity is suitably in the range of 0.5 to 3 volumes of tertiary butyl hydroperoxide charge stock per volume of catalyst per hour. Preferably, the space velocity is within the range of 1 to 2 volumes of tertiary butyl hydroperoxide charge stock per volume of catalyst per hour. The reaction product from the tertiary butyl hydroperoxide decomposition step may then be fractionated in any suitable manner, such as by distillation to recover the tertiary butyl alcohol. EXAMPLES The invention will be further illustrated by the following non-limiting examples. Procedure The reactor was a stainless steel tube (12.3 x 360mm) which was electrically heated. Liquid feed was pumped into the bottom of the reactor. Pressure regulation was with a Skinner Uni-Flow® valve and a Foxboro® controller. The liquid feed was pumped with a Ruska® dual drive pump. 20% TBHP was prepared from 55% isobutane peroxidation reactor effluent by diluting with commercial TBA. Analysis of the reactor effluent was by Gas Chromatograpy. Details are given in the following tables: Example 1 In this example, the catalyst consisted essentially of pelleted titania or zirconia. CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 1 2 3 4 Catalyst Norton TiO 2 Norton TiO 2 Norton TiO 2 Norton TiO 2 Catalyst (cc) 100 100 100 100 Pressure (MPa) 3.5 3.5 3.5 3.5 Feed Rate (cc/Hr.) 50 50 50 50 Temperature (°C) 80 100 120 140 Time on Stream (Hr) 4 4 4 4 Space Vel. (cc/cc) 0.5 0.5 0.5 0.5 TBHP Conversion (mol.%) 22.5 72.0 92.7 98.5 Selectivity IC4= (mol.%) 0.3 0.2 0.1 1.5 Sel. Acetone (mol.%) 11.6 16.4 31.0 32.8 Sel. Methanol (mol.%) 1.3 3.3 8.5 8.9 Sel. TBA (mol.%) 80.5 79.3 66.4 66.1 Sel. DTBP (mol.%) 7.9 4.3 2.5 1.1 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.009 0.014 0.008 0.172 MEOH/MF 0.016 0.036 0.178 0.553 0.614 Acetone 0.008 0.329 1.465 3.559 3.994 TBA 79.968 83.753 91.494 93.449 93.754 DTBP 0.055 0.330 0.531 0.419 0.230 TBHP 19.146 14.843 5.356 1.395 0.288 CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 5 6 7 Catalyst Norton TiO 2 Norton TiO 2 Norton TiO 2 Catalyst (cc) 100 100 100 Pressure (MPa) 3.5 3.5 3.5 Feed Rate (cc/Hr.) 100 100 100 Temperature (°C) 100 120 140 Time on Stream (Hr) 4 4 4 Space Vel. (cc/cc) 1.0 1.0 1.0 TBHP Conversion (mol.%) 35.8 89.2 99.5 Selectivity IC4= (mol.%) 0.2 0.7 2.1 Sel. Acetone (mol.%) 13.0 27.5 40.6 Sel. Methanol (mol.%) 2.6 8.1 10.5 Sel. TBA (mol.%) 82.2 70.4 59.3 Sel. DTBP (mol.%) 4.8 2.1 0.2 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.009 0.077 0.245 MEOH/MF 0.016 0.080 0.507 0.726 Acetone 0.008 0.583 3.037 4.993 TBA 79.968 85.597 93.102 92.353 DTBP 0.055 0.322 0.342 0.079 TBHP 19.146 12.289 2.067 0.091 CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 8 9 10 Catalyst Norton TiO 2 Norton TiO 2 Norton TiO 2 Catalyst (cc) 100 100 100 Pressure (MPA) 3.5 3.5 3.5 Feed Rate (cc/Hr.) 200 200 200 Temperature (°C) 100 120 140 Time on Stream (Hr) 4 4 4 Space Vel. (cc/cc) 2.0 2.0 2.0 TBHP Conversion (mol.%) 16.4 55.1 89.0 Selectivity IC4= (mol.%) 0.4 0.4 2.4 Sel. Acetone (mol.%) 14.1 20.0 36.2 Sel. Methanol (mol.%) 2.3 3.5 11.7 Sel. TBA (mol.%) 80.7 76.9 62.8 Sel. DTBP (mol.%) 5.2 3.0 1.0 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.008 0.027 0.252 MEOH/MF 0.016 0.042 0.146 0.723 Acetone 0.008 0.293 1.370 3.984 TBA 79.968 82.401 88.264 91.443 DTBP 0.055 0.188 0.314 0.190 TBHP 19.146 16.000 8.597 2.114 CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 11 12 13 14 Catalyst Norton ZrO 2 Norton ZrO 2 Norton ZrO 2 Norton ZrO 2 Catalyst (cc) 100 100 100 100 Pressure (MPa) 3.5 3.5 3.5 3.5 Feed Rate (cc/Hr.) 50 50 50 50 Temperature (°C) 80 100 120 140 Time on Stream (Hr) 4 4 4 4 Space Vel. (cc/cc) 0.5 0.5 0.5 0.5 TBHP Conversion (mol.%) 19.7 77.5 100.0 100.0 Selectivity IC4= (mol.%) 0.0 0.0 0.1 0.1 Sel. Acetone (mol.%) 10.8 15.8 30.2 32.5 Sel. Methanol (mol.%) 1.3 3.8 7.8 7.3 Sel. TBA (mol.%) 81.1 79.2 67.5 66.4 Sel. DTBP (mol.%) 8.2 5.0 2.3 1.1 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.001 0.004 0.008 0.013 MEOH/MF 0.016 0.034 0.216 0.545 0.511 Acetone 0.008 0.270 1.523 3.733 4.018 TBA 79.968 83.121 92.713 94.030 94.347 DTBP 0.055 0.305 0.656 0.417 0.220 TBHP 19.146 15.373 4.302 0.000 0.000 CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 15 16 17 Catalyst Norton ZrO 2 Norton ZrO 2 Norton ZrO 2 Catalyst (cc) 100 100 100 Pressure (MPa) 3.5 3.5 3.5 Feed Rate (cc/Hr.) 100 100 100 Temperature (°C) 100 120 140 Time on Stream (Hr) 4 4 4 Space Vel. (cc/cc) 1.0 1.0 1.0 TBHP Conversion (mol.%) 53.9 95.9 96.9 Selectivity IC4= (mol.%) 0.0 0.5 0.2 Sel. Acetone (mol.%) 13.7 26.8 35.6 Sel. Methanol (mol.%) 3.3 6.8 8.2 Sel. TBA (mol.%) 80.8 70.9 63.6 Sel. DTBP (mol.%) 5.6 2.3 0.8 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.002 0.057 0.022 MEOH/MF 0.016 0.138 0.459 0.558 Acetone 0.008 0.916 3.183 4.258 TBA 79.968 88.872 94.379 93.539 DTBP 0.055 0.522 0.401 0.177 TBHP 19.146 8.827 0.781 0.602 CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL RUN A 18 19 20 Catalyst Norton ZrO 2 Norton ZrO 2 Norton ZrO 2 Catalyst (cc) 100 100 100 Pressure (MPa) 3.5 3.5 3.5 Feed Rate (cc/Hr.) 200 200 200 Temperature (°C) 100 120 140 Time on Stream (Hr) 4 4 4 Space Vel. (cc/cc) 2.0 2.0 2.0 TBHP Conversion (mol.%) 28.9 83.0 94.9 Selectivity IC4= (mol.%) 0.0 -0.0 0.1 Sel. Acetone (mol.%) 13.4 11.6 34.0 Sel. Methanol (mol.%) 3.1 7.0 8.6 Sel. TBA (mol.%) 80.4 85.8 65.3 Sel. DTBP (mol.%) 6.2 2.6 0.7 Remarks H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis H 2 O Free Basis Composition, wt% IC4= 0.001 0.002 0.000 0.011 MEOH/MF 0.016 0.076 0.410 0.575 Acetone 0.008 0.486 1.201 3.992 TBA 79.968 84.554 94.037 93.362 DTBP 0.055 0.331 0.386 0.159 TBHP 19.146 13.615 3.252 0.967 Example 2 A 19.1% solution of TBHP in TBA decomposed over a heterogeneous zirconium or titanium catalyst gave good yields of TBA. For example, using a 50 cc up-flow reactor at 100°C and a space velocity of 0.5, a commercial titanium oxide catalyst gave 72.0% TBHP conversion and a selectivity to TBA of 79.3%. The selectivity to acetone was 16.4%, methanol 3.3% and DTBP 4.3%. Under the same conditions a commercial zirconium oxide catalyst gave 77.5% TBHP conversion and a selectivity to TBA of 79.2%. The selectivity to acetone was 15.8%, methanol 3.8% and DTBP 5.0%. Minor products including carboxylic acids were also formed.

Claims: A method for the decomposition of tertiary butyl hydroperoxide to tertiary butyl alcohol, wherein a solvent solution of a tertiary butyl hydroperoxide charge stock is brought into contact with a hydroperoxide decomposition catalyst, characterized in that said hydroperoxide decomposition catalyst comprises titania or zirconia or a mixture thereof. A method as claimed in Claim 1, wherein the solvent comprises tertiary butyl alcohol, or a mixture thereof with isobutane A method as claimed in Claim 1 or Claim 2, wherein a solution of a tertiary butyl hydroperoxide charge stock that contains from 5 to 30 wt.% of tertiary butyl hydroperoxide is brought into contact with a catalytically effective amount of a hydroperoxide decomposition catalyst in a hydroperoxide decomposition reaction zone in liquid phase under hydroperoxide conversion conditions including a temperature within the range of 20° to 250°C. and a pressure of 0.1 to 7 MPa (0 to 1,000 psig) to convert said tertiary butyl hydroperoxide to decomposition products, principally tertiary butyl alcohol. A method as claimed in anyone of Claims 1 to 3, wherein the temperature is in the range of 60° to 120°C and the pressure is 0.1 MPa to 7.0 MPa. A method as claimed in anyone of Claims 1 to 4, wherein the catalyst consists essentially of titania. A method as claimed in anyone of Claims 1 to 4, wherein the catalyst consists essentially of zirconia.

Inventors: KNIFTON JOHN FREDERICK, MARQUIS EDWARD THOMAS, SANDERSON JOHN RONALD, KNIFTON, JOHN FREDERICK, MARQUIS, EDWARD THOMAS, SANDERSON, JOHN RONALD
Applicants: TEXACO DEVELOPMENT CORP, TEXACO DEVELOPMENT CORPORATION
Application year: 1994
Main classification: C07C29
IPC codes: C07C31, C07C29, C07C27, C07B61, B01J21